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WO1993007092A1 - Systeme de bioreacteur a membranes pour le traitement de fluides synthetiques issus de la transformation des metaux et de produits a base d'huile - Google Patents

Systeme de bioreacteur a membranes pour le traitement de fluides synthetiques issus de la transformation des metaux et de produits a base d'huile Download PDF

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Publication number
WO1993007092A1
WO1993007092A1 PCT/CA1992/000442 CA9200442W WO9307092A1 WO 1993007092 A1 WO1993007092 A1 WO 1993007092A1 CA 9200442 W CA9200442 W CA 9200442W WO 9307092 A1 WO9307092 A1 WO 9307092A1
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WIPO (PCT)
Prior art keywords
solids
zone
wastewater
permeate
membrane
Prior art date
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Ceased
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PCT/CA1992/000442
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English (en)
Inventor
Fernando A. Tonelli
Philip R. Canning
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GE Zenon ULC
Original Assignee
Zenon Environmental Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Zenon Environmental Inc filed Critical Zenon Environmental Inc
Priority to DK93906356T priority Critical patent/DK0560980T3/da
Priority to AU27505/92A priority patent/AU663893B2/en
Priority to KR1019930701720A priority patent/KR0177184B1/ko
Priority to SK58393A priority patent/SK58393A3/sk
Priority to PL29982792A priority patent/PL299827A1/xx
Priority to CS931124A priority patent/CZ112493A3/cs
Priority to EP19930906356 priority patent/EP0560980B1/fr
Priority to DE69223609T priority patent/DE69223609T2/de
Publication of WO1993007092A1 publication Critical patent/WO1993007092A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/0208—Separation of non-miscible liquids by sedimentation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/0208—Separation of non-miscible liquids by sedimentation
    • B01D17/0214—Separation of non-miscible liquids by sedimentation with removal of one of the phases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/04—Breaking emulsions
    • B01D17/047—Breaking emulsions with separation aids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/08—Thickening liquid suspensions by filtration
    • B01D17/085—Thickening liquid suspensions by filtration with membranes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/24—Feed or discharge mechanisms for settling tanks
    • B01D21/2433—Discharge mechanisms for floating particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/24—Feed or discharge mechanisms for settling tanks
    • B01D21/2444—Discharge mechanisms for the classified liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/30—Control equipment
    • B01D21/305—Control of chemical properties of a component, e.g. control of pH
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1205—Particular type of activated sludge processes
    • C02F3/1231—Treatments of toxic sewage
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • C10M175/06—Working-up used lubricants to recover useful products ; Cleaning by ultrafiltration or osmosis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • an aerobic bioreactor is highly sensitive to the composition of wastewater treated and the time within which treatment is to be completed. Stated differently, given enough time and no reasonable constraint on the expenditure of energy, the challenge to operate a waste treatment system would be de minimis. Since the challenge is to provide a system which economically satisfies the time-energy sensitivity of its operation, the emphasis in the art is to provide the most efficient means to maintain the activity of a biomass by transferring as much oxygen into the bioreactor's reaction mass (aqueous suspension of biomass, namely, of organic solids and microorganisms) as can be used by microorganisms to biodegrade biochemically oxidizable material.
  • aqueous suspension of biomass namely, of organic solids and microorganisms
  • this invention relates to treating a mixture of natural hydrocarbon and synthetic metal-working fluids, fats, oils and greases ("FOG”) mixed with synthetic organic and organometallic compounds, some of which are insoluble solids, others emulsifiable liquids, and still others soluble solids and liquids.
  • This mixture in wastewater is referred to herein as "waste fluids”.
  • Waste fluids comprise particularly difficult-to-treat components and relatively easy-to-treat components.
  • the problem is to provide a process which will biologically degrade waste fluids in a wastewater stream which varies from one hour to the next, economically.
  • the stream varies both in mass flow per hour, and in the concentration of waste fluids therein.
  • the problem to be solved is to use a membrane separator which typically operates with constant mass flow per hour, in conjunction with a bioreactor, to provide an effluent which will meet governmental compliance requirements.
  • the ratios of the components of the waste fluids varies during operation.
  • a successful process requires that it operate essentially continuously substantially without human attention. Still further, the waste production from the process is to be minimized.
  • the process incorporates the foregoing features and relies upon the unique operation, in combination, of an ambient pressure aerobic reactor, an equalization tank, and a membrane device tailored to let pass through it, a predetermined amount and size of molecules which are the product of biodegradation.
  • Wastewater delivered (“delivered wastewater”) is pretreated to remove floatable free oil and settleable solids prior to transfer into an equalization tank.
  • a pretreatment device is a corrugated plate interceptor (CPI) although any other devices suitable for removing floatable oils and settleable solids may be used.
  • CPI corrugated plate interceptor
  • the removal of floatable free oils and settleable solids may be performed in the equalization tank directly, with suitable equipment.
  • the feed to the bioreactor is taken from the equalization tank and contains FOG having chemical and physical properties quite unlike wastewater containing waste generated by human activities, typical of municipal wastewater.
  • wastewater from metal-working operations contain any or all of the following constituents: petroleum-based (oil-based) FOG; non-petroleum based (synthetic or semi-synthetic oils) FOG; and organometallic compounds. These constituents vary in biodegradability across the full spectrum of difficulty. It is this feed which was treated in a membrane bioreactor system which was extensively tested at the NDH General Motors automobile plant, in the pilot plant tests which were reported in a paper presented on October 10, 1990 at the WPCF Conference in Washington, D.C.
  • the essential process characteristic of the '765 process was that it maintained a constant reactor volume by varying the feed flow. Further, the organic solids were comminuted but not removed, so they remained in the recycled concentrate. In contrast, the process of our invention maintains a constant reactor volume by maintaining the flow rate of feed to the reactor essentially constant, and, recycling both concentrate and permeate. In our process, essentially no solids greater than about 106 ⁇ m enter the reactor, and the only solids in the system are the aforementioned finely divided organic solids, the biomass
  • the '765 system was commercialized with limited
  • each mechanical component in the system is known, the combination used in our process is found to be effective if operated as described hereunder to treat delivered wastewater which contains a very high concentration of FOG.
  • the bioreactor is operated to maintain a predetermined concentration of FOG and total suspended solids ("TSS"), and the membrane device is operated as an ultrafiltration membrane at low pressure, in the range from about 170 to 1035 Kpa (25 psig to 150 psig).
  • TSS total suspended solids
  • the mass flow from the bioreactor is surprisingly high, yet (i) provides a long solids retention time (SRT), and enough liquid as is required per unit of air entrained, to degrade the FOG in delivered wastewater, and also (ii) completes degradation of the organic waste with a hydraulic retention time of less than 5 days, preferably less than 48 hr, in the bioreaction system.
  • SRT solids retention time
  • the key to providing the foregoing is to retain emulsified pollutants for a period longer than the liquid residence time or hydraulic retention time (HRT) of the reactor, based on the wastewater flow rate.
  • This pretreated wastewater allows the bioreactor in combination with an ultrafiltration membrane means, to be operated with a hydraulic retention time (HRT) of at least 24 hr, preferably from 1 to 5 days, and a solids retention time (SRT) in the range from about 30-150 days, preferably from 50 - 125 days.
  • HRT hydraulic retention time
  • SRT solids retention time
  • waste fluids generated in a metal-working facility can be successfully biodegraded if solids are first removed from delivered wastewater, the mass flow of feed to the bioreaction zone is maintained substantially constant, the hydraulic retention time (HRT) is maintained in the range from about 24 - 48 hr, and the solids retention time (SRT) is maintained greater than 30 days, preferably at least 50 days. Effectively, the emulsified pollutants are retained for a period longer than the HRT of the bioreaction zone, based on the flow rate of wastewater.
  • HRT hydraulic retention time
  • SRT solids retention time
  • Figure 1 is a simplified flowsheet of a membrane-bioreactor system schematically showing its operation with two ultrafiltration modules, and the essential permeate
  • Figure 2 is a graph showing the variation of membrane flux as a function of time.
  • Figure 3 is a graph showing the build-up of suspended solids in the bioreactor due to inert solids over nearly a year, at various levels of inert solids concentration in the wastewater feed (g/L).
  • the membrane-bioreactor system is intended for use by those concerned with the cost of treating wastewater generated in a metal-working plant effectively.
  • this wastewater is a relatively small volume compared to the volume of biodegradable waste generated by a metropolitan area, the difficulty of disposing of it requires that it be disposed of by the operators of the plant.
  • the delivered wastewater from such a plant cannot be treated in a municipal sewage disposal facility because of the poor biodegradability of waste fluids in the wastewater.
  • the required membrane area is based on minimum flux, as before, and is 10 m 2 .
  • the reactor volume is based on minimum flux 100 L/m 2 -hr, since feed flow is constant and both concentrate and permeate are recycled, so the volume of the reactor now required is
  • ⁇ Yk - b (1)
  • ⁇ organism specific growth rate, mass/mass-time
  • the organism specific growth rate is equal to the reciprocal of the SRT of the system.
  • VSS lost in the effluent or intentionally wasted/day and, Yn net organism yield coefficient.
  • the SRT is controlled by wasting a predetermined volume of the contents of the reactor, per day.
  • k After establishing the SRT deemed necessary to achieve a given effluent quality, along with values for Y and b, or Yn, k can be determined. With k known, the required reactor volume can be determined from values for the reactor VSS and feed and effluent concentration values.
  • the SRT and HRT of an optimal reactor depends on the molecular size of the wastewater components and reaction products, the biological and chemical (hydrolysis reactions) treatability characteristics of the wastewater components, the inhibitory nature of the reaction products, and the membrane characteristics with respect to effective pore size.
  • J depends on such factors as the reactor TSS, surface velocity, temperature, transmembrane pressure drop, surface fouling and the extent of concentration polarization.
  • Concentration polarization arises from the accumulation of solutes on the membrane surface. Solutes reach the membrane surface by convective transport of the solvent, a portion of which passes through the membrane. The rejected solutes often form a viscous gel layer on the membrane. This gel layer acts as a secondary membrane reducing the flux and often reducing the passage of low molecular weight solutes. Surface fouling is the result of the deposition of submicron particles on the surface as well as the accumulation of smaller solutes due to such processes as crystallization and precipitation. It is this deterioration in membrane flux which is counteracted by using a larger membrane area than is necessary, and by recycling permeate to the bioreactor.
  • a bioreactor 10 which contains an aqueous suspension 12 of live
  • microorganisms which have been especially acclimated to ingest the waste fluids as nutrients, albeit with the deliberate addition of other "added” nutrients such as phosphate and nitrogenous compounds.
  • the nutrient value of the waste fluids is typically so poor as to require continuous addition of the added nutrients to help the microorganisms ingest the waste fluids.
  • Such microorganisms are commercially available.
  • the bioreactor operates at atmospheric pressure; it is provided with a sparger 14 through which air or oxygen required to maintain the microorganisms, is distributed from conduit 13 uniformly throughout the reactor.
  • the reactor includes baffle means to improve contacting the waste fluids with the microorganisms.
  • Delivered wastewater is introduced through line 15 in to an equalization tank 20 which, in addition to equalizing the flow to the reactor, also serves as a settling tank for the removal of settled solids through line 17, and the removal of free oil through line 11.
  • Free oil and grease "skim" 16 float to the surface and are skimmed off.
  • Solids 17 settle and are either periodically or continuously removed from the bottom of the settling tank, depending upon the level of solids in the delivered wastewater, and disposed of.
  • the aqueous suspension of wastewater from the settling tank 20 is withdrawn through line 21 and 22 before it is led to the suction side of a feed pump 24 which operates at low pressure to pump the aqueous suspension of equalized wastewater through about a 106 ⁇ m filtration unit 26.
  • the filtered aqueous suspension is then led through conduit 23 into the bioreactor 10.
  • Feed to the bioreactor 10 is maintained essentially constant so as to maintain a predetermined concentration of solids in the mass 12, and liquid level in the bioreactor.
  • a stream of the contents 12 of the bioreactor is withdrawn through pump suction line 27 and discharged as a pressurized stream by pressurization pump 28 through a discharge line 29 to a membrane filtration unit indicated generally by reference numeral 30.
  • a membrane filtration unit 30 having two or more ultrafiltration modules 31 and 32 connected in parallel, in each of which the membrane has a pore size smaller than 0.5 ⁇ m, and to maintain operation of the membrane unit 30 with a clean water flux (measured at 20°C and 40 psig or 370 kPa abs) of at least 10 m 3/m2/day.
  • Permeate from the membrane unit 30 is removed from the system through permeate recycle conduit 33, while concentrate leaves through concentrate recycle conduit 35.
  • the outlet pressure of the concentrate in line 29 is in the range from about 250 kPa (25 psig) to about 1000 kPa (125 psig) depending upon the configuration of the modules and layout of the membrane units.
  • a major portion, preferably more than 95% by volume, of the concentrate stream flowing through conduit 35 is recycled as recycle stream 37 and the remainder 37' purged through purge line 37.
  • a minor portion, preferably from about 0.1% to 30% by volume, of the permeate stream flowing through conduit 33 is recycled as recycle stream 39 and the remainder withdrawn as treated effluent through effluent line 39'.
  • the volume of effluent permeate removed through line 39' will depend upon the physical characteristics of the reaction mass as well as the specifications of the
  • the effluent stream 33 will range from about 0.5% by volume or even less, to about 3% by volume of the pressurized bioreactor contents stream 29.
  • the portion 39 of the permeate recycled to the bioreactor maintains a balance between incoming feed to the membrane device and removed effluent.
  • a portion of the recycle streams 37 and 39 may be diverted to a cleaning tank 40 through conduits 41 and 43 respectively, and used to wash and chemically clean the membranes when required.
  • One or more chemicals addition tanks 44 are provided to supply acid and alkali for pH control, and various nutrients, for example phosphate, to supplement the nutrients provided to the biomass by the waste fluids.
  • Pump(s) 45 meter the appropriate chemical(s) when desired *
  • a membranous filtration unit preferably has a pore size in the range from about 0.001 ⁇ m to about 0.05 ⁇ m, but may be larger, from about 0.01 ⁇ m to about 0.1 ⁇ m, if lesser quality effluent is acceptable.
  • Preferred membranes for microfiltration are derived from poly(vinyl alcohol), polysulfone, polypropylene, nylon and the like, for example Zenon SJ.
  • the same materials may be used to provide ultrafiltration membranes, for example a Zenon TAM membrane.
  • Fig 2 it is evident that the modules operated for over a year without having to be replaced.
  • the flux varied over more than a two-fold range from about 16 gals/ft 2 -day to 42 gals/ft 2 -day.
  • the bacteria found to be effective in the process are commonly found in activated sludge and include the genera Pseudomonas, Zooglea, Achromobacter, Flavobacter, Nocardia, Bdellovibrio, and Mycobacter, normally all considered heterotrophic. These perform the bulk of the bio-stabilization.
  • the autotrophic bacteria which may be present are represented by Nitrosonomas and Nitrobacter, both nitrogen fixing. Also found in activated sludge are a variety of fungus, yeasts and protozoa, some of which are also useful in our process.
  • a 3.78 m 3 (1000 gal) bioreactor is operatively connected with a variable module.
  • multi-tube membrane unit of Zenon Z8 modules with HSC or TAM membranes Each module contained 8 1.83 m long by 2.22 cm diameter tubes connected in series to provide a membrane area of 0.975 m 2 /module.
  • the modules themselves were connected in parallel with the concentrate recycle to the bioreactor, and with the permeate being recycled to the bioreactor and being removed as effluent.
  • a liquid level control system maintains the reactor volume within 11 percent of the mean reactor volume. Enough air was introduced into the reactor to provide complete mixing and aerobic conditions for growth of the biomass.
  • the daily mean dissolved oxygen (DO) concentration in the reactor was in the range from 0.5 to 6.1 mg/L.
  • the reactor pH ranged from 6.8 to 7.9.
  • the ratio of concentrate recycle Q c to permeate flow Q p is maintained at about 120.
  • the concentration of solids in the concentrate recycle line is essentially the same as that in the bioreactor.
  • Membrane-Bioreactor System Start-up: The reactor is seeded with biomass together with a small amount of nutrients (nitrogen, phosphorus, potassium) if required, to support biomass growth, and air flow was adjusted to maintain an excess concentration of dissolved oxygen.
  • the reactor pH was maintained near neutral by addition of sulfuric acid. Automatic pH control is maintained with a set point of 7.5.
  • TSS represents total
  • FOG fats, oils and grease.
  • a further reduction in accumulation of high mol wt, soluble and non-reactive compounds can be achieved by using a more open membrane such as the Zenon TAM membrane, than the Zenon HSC membrane used for the other runs.
  • Solids balances were completed across the membrane system at each equilibrium condition in order to determine biomass net yield coefficients.
  • the low yield values observed are attributable to the long SRTs used in this process. These values are set forth in Table V below.
  • the mass balance information can be used to estimate the solids produced per volume of wastewater treated in the system. A value of 0.21 kg/m 3 (1.78 lb/1000 gal) of wastewater treated was determined, based on the average net yield value observed. This value is less than 10% of the solids that would be produced from a conventional physical-chemical oily wastewater treatment system with conventional add-on biological treatment. TABLE IV. Effect on MBR system performance of using a more
  • HSC membrane TAM membrane (R un P3-2) (day 271 to day 287)
  • the membrane flux of the unit was approximately 100 L/m 2 -hr (59 gal/ft 2 - day) upon start-up of the system. The flux declined rapidly over approximately the first forty days and after that, averaged between 40 - 50 L/m 2 -hr. The membranes were cleaned with alkali every one or two weeks to restore the flux to approximately 60 L/m 2 -hr.
  • the membrane unit was operated until day 196 with minimal back pressure exerted on the membranes by the discharge pressure control valve.
  • the pressure at the exit of the membrane unit was less than 70 kPa (10 psig).
  • the pressure was increased to 140 kPa (20 psig) to bring the system in line with anticipated full scale operating conditions. As a result of the increase of pressure there was also a 14-20% increase in flux.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Health & Medical Sciences (AREA)
  • Toxicology (AREA)
  • Combustion & Propulsion (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Fats And Perfumes (AREA)
  • Activated Sludge Processes (AREA)

Abstract

On décrit un système de traitement des eaux usées utilisé dans une installation de transformation des métaux, telle qu'une usine de fabrication d'automobiles, ce traitement se faisant dans un bioréacteur utilisant des microorganismes vivants. Ces eaux usées contiennent des fluides résiduaires qui sont un mélange de matières grasses et d'huiles relativement facilement biodégradables, des fluides synthétiques, des huiles et des graisses bien moins facilement biodégradables, et des matières non-biodégradables comprenant des solides inorganiques finement divisés tels que des particules de métal et de carbure de silicium. Ces fluides résiduaires exigent un temps de rétention hydraulique (TRH) et un temps de rétention de solides (TRS) 10 fois plus élevé que les eaux d'égout. L'eau de qualité supérieure est séparée des solides en suspension qui sont éliminés du réacteur à une vitesse essentiellement constante et amenés à une membrane d'ultrafiltration. Le concentré est recyclé vers le réacteur, excepté un courant de purge, pour éliminer périodiquement les solides. Les membranes acquièrent une durée de vie longue et efficace malgré les grandes variations du flux de la membrane grâce à un recyclage du perméat qui permet au bioréacteur de fonctionner à volume constant, aux eaux usées d'alimentation de s'écouler vers le réacteur à vitesse constante, et aux modules à membrane de fonctionner à une pression relativement basse, à un régime restreint pour ne pas endommager les membranes. Ce type de fonctionnement du bioréacteur permet d'utiliser un réacteur dont la taille (volume) est la moitié de celle exigée dans un système sans recyclage de perméat. On obtient un fonctionnement efficace et durable des membranes en filtrant (par un écran de 140 meshs) tous les solides dont le diamètre est supérieur à environ 106 νm. Des essais dans des installations pilotes effectués sur des eaux usées provenant d'usines de fabrication d'automobiles, menés sur une période de plus d'un an, mettent en évidence l'efficacité surprenante du système sur une période prolongée.
PCT/CA1992/000442 1991-10-09 1992-10-09 Systeme de bioreacteur a membranes pour le traitement de fluides synthetiques issus de la transformation des metaux et de produits a base d'huile Ceased WO1993007092A1 (fr)

Priority Applications (8)

Application Number Priority Date Filing Date Title
DK93906356T DK0560980T3 (da) 1991-10-09 1992-10-09 Membran-bioreaktor-system til behandling af syntetiske fluider fra metalbearbejdning og oliebaseredeprodukter
AU27505/92A AU663893B2 (en) 1991-10-09 1992-10-09 Membrane bioreactor system for treating synthetic metal-working fluids and oil-based products
KR1019930701720A KR0177184B1 (ko) 1991-10-09 1992-10-09 합성 금속처리용액 및 오일-기초 제품을 처리하기 위한 여과막-생물반응기 시스템
SK58393A SK58393A3 (en) 1991-10-09 1992-10-09 Membrane bioreactor system for treating synthetic metal-working fluids and oil-based products
PL29982792A PL299827A1 (en) 1991-10-09 1992-10-09 Membrane reactor arrangement for purification of synthetic fluids used in metal machining and working processes as well as other oil-based products
CS931124A CZ112493A3 (en) 1991-10-09 1992-10-09 Process and apparatus with a membrane bio-aerating tank for treating waste water, particularly synthetic liquids used when cutting metals and products based on oil
EP19930906356 EP0560980B1 (fr) 1991-10-09 1992-10-09 Systeme de bioreacteur a membranes pour le traitement de fluides synthetiques issus de la transformation des metaux et de produits a base d'huile
DE69223609T DE69223609T2 (de) 1991-10-09 1992-10-09 Membranbioreaktorsystem zur behandlung von synthetischen metallbearbeitungsfluessigkeiten und produkten auf oel-basis

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US07/773,226 US5204001A (en) 1991-10-09 1991-10-09 Membrane bioreactor system for treating synthetic metal-working fluids and oil-based products
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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1997005071A1 (fr) * 1995-07-27 1997-02-13 Helmut Hohnecker Procede pour la decontamination biologique de materiaux contamines
EP0735005A3 (fr) * 1995-03-27 1997-10-15 Zenon Environmental Inc Procédé de traitement de composés difficilement biodégradables
US6649665B2 (en) 2000-11-15 2003-11-18 Nippon Shokubai Co., Ltd. Method for production of porous cross-linked polymer material
CN102107993A (zh) * 2010-12-23 2011-06-29 郑高宽 一种过滤多种水源成直饮水的方法
CN101402492B (zh) * 2008-11-19 2011-06-29 北京桑德环境工程有限公司 提高回收率的废水处理系统及处理方法

Families Citing this family (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5204001A (en) * 1991-10-09 1993-04-20 Zenon Environmental Inc. Membrane bioreactor system for treating synthetic metal-working fluids and oil-based products
US5403490A (en) * 1992-11-23 1995-04-04 Desai; Satish Process and apparatus for removing solutes from solutions
JP2606156B2 (ja) * 1994-10-14 1997-04-30 栗田工業株式会社 研磨剤粒子の回収方法
DE19613397C2 (de) * 1996-04-03 2000-06-08 Fraunhofer Ges Forschung Verfahren zum biologischen Reinigen von Abwasser
US6007712A (en) * 1997-02-28 1999-12-28 Kuraray Co., Ltd. Waste water treatment apparatus
US6168712B1 (en) * 1998-05-06 2001-01-02 Kenko Sangyo Co., Ltd. Apparatus for the biological treatment of waste fluid from the coating process
US6248985B1 (en) 1998-06-01 2001-06-19 Stericycle, Inc. Apparatus and method for the disinfection of medical waste in a continuous manner
JP2000084567A (ja) * 1998-09-11 2000-03-28 Fuji Heavy Ind Ltd 切削油含有廃水の処理方法
NL1013097C2 (nl) * 1999-09-20 2001-03-21 Wijngaart Adriaan J Van Der Mestbewerking en/of -verwerking.
ATE237561T1 (de) * 1999-10-26 2003-05-15 Rochem Ultrafiltrations System Verfahren zur reinigung und/oder aufbereitung kommunaler und/oder industrieller abwässer
US6299766B1 (en) * 2000-07-06 2001-10-09 Clark Permar Reverse osmosis filtering apparatus with concentrate dilution
US6706171B2 (en) 2000-10-12 2004-03-16 Biochem Technology, Inc. Systems for treating wastewater in a series of filter-containing tanks
US6780318B2 (en) * 2000-10-30 2004-08-24 Jerome Jay Fife Method for recovering a disposal trench with a biomat slime, and method for operating a waste treatment vessel
FR2847572B1 (fr) * 2002-11-22 2006-04-21 Omnium Traitement Valorisa Procede de traitement des eaux a l'aide d'un reactif pulverulent inorganique a forte surface specifique incluant une etape de recyclage dudit reactif
US20040226887A1 (en) * 2003-05-15 2004-11-18 The Board Of Trustees Of The University Of Illinois High percentage recovery method for purifying microemulsions
WO2006002529A1 (fr) * 2004-07-01 2006-01-12 Zenon Technology Partnership Appareil de filtrage pour le traitement de l'eau au moyen de membranes
US7455777B2 (en) * 2004-12-14 2008-11-25 Itt Manufacturing Enterprises, Inc. Method of adjusting levels of dissolved compounds in beverages
US20080011693A1 (en) * 2006-07-12 2008-01-17 Ming Li Self-cleaning waste-water device and method
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US20090223891A1 (en) * 2008-03-06 2009-09-10 Ray Gauthier System, device and method for on-site wastewater processing
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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3740211A1 (de) * 1986-12-09 1988-07-28 Volkswagen Ag Verfahren zur wiederaufbereitung von verschmutzten alkalischen gleitschleifwaessern von gleitschleifanlagen
DE3709174A1 (de) * 1987-03-20 1988-09-29 Wehrle Werk Ag Verfahren und vorrichtung zur biologischen reinigung von organisch belasteten abwaessern
WO1990015028A1 (fr) * 1989-06-05 1990-12-13 Ab Institutet För Vatten- Och Luftvårdsforskning Procede de traitement biologique d'eaux residuelles

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3472765A (en) * 1968-06-10 1969-10-14 Dorr Oliver Inc Membrane separation in biological-reactor systems
US4655928A (en) * 1983-10-18 1987-04-07 Gnb Incorporated Membrane processes for metal recovery and pollution control in metal process industries
US4749494A (en) * 1985-04-01 1988-06-07 Mitsui Sekiyu Kagaku Kogyo Kabushiki Kaisha Treatment of waste water by the activated sludge process
DE3544383A1 (de) * 1985-07-17 1987-01-29 Ivan Sekoulov Verfahren zur biologischen und/oder physikalischen elimination unerwuenschter wasserinhaltsstoffe aus wasser mittels gefluteter biofilmreaktoren u. anlage zur durchfuehrung des verfahrens
FR2594113B1 (fr) * 1986-02-07 1991-05-17 Degremont Procede et installation pour l'epuration d'eaux residuaires, notamment d'eaux residuaires urbaines
US4904387A (en) * 1988-06-17 1990-02-27 Thetford Corporation Waste treatment and water recycling toilet system
US5204001A (en) * 1991-10-09 1993-04-20 Zenon Environmental Inc. Membrane bioreactor system for treating synthetic metal-working fluids and oil-based products

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3740211A1 (de) * 1986-12-09 1988-07-28 Volkswagen Ag Verfahren zur wiederaufbereitung von verschmutzten alkalischen gleitschleifwaessern von gleitschleifanlagen
DE3709174A1 (de) * 1987-03-20 1988-09-29 Wehrle Werk Ag Verfahren und vorrichtung zur biologischen reinigung von organisch belasteten abwaessern
WO1990015028A1 (fr) * 1989-06-05 1990-12-13 Ab Institutet För Vatten- Och Luftvårdsforskning Procede de traitement biologique d'eaux residuelles

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
JOURNAL OF WATER POLLUTION CONTROL vol. 46, no. 9, September 1974, pages 2183 - 2192 R. L. GOLDSMITH ET AL. 'ULTRAFILTRATION OF SOLUBLE OIL WASTES' *

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0735005A3 (fr) * 1995-03-27 1997-10-15 Zenon Environmental Inc Procédé de traitement de composés difficilement biodégradables
WO1997005071A1 (fr) * 1995-07-27 1997-02-13 Helmut Hohnecker Procede pour la decontamination biologique de materiaux contamines
US6649665B2 (en) 2000-11-15 2003-11-18 Nippon Shokubai Co., Ltd. Method for production of porous cross-linked polymer material
CN101402492B (zh) * 2008-11-19 2011-06-29 北京桑德环境工程有限公司 提高回收率的废水处理系统及处理方法
CN102107993A (zh) * 2010-12-23 2011-06-29 郑高宽 一种过滤多种水源成直饮水的方法
CN102107993B (zh) * 2010-12-23 2014-08-20 郑高宽 一种过滤多种水源成直饮水的方法

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AU663893B2 (en) 1995-10-26
SK58393A3 (en) 1993-10-06
CZ112493A3 (en) 1994-01-19
DE69223609D1 (de) 1998-01-29
KR0177184B1 (ko) 1999-04-01
HUT73571A (en) 1996-08-28
HU9301834D0 (en) 1993-11-29
DE69223609T2 (de) 1998-07-16
PL299827A1 (en) 1994-01-24
CN1075938A (zh) 1993-09-08
EP0560980B1 (fr) 1997-12-17
CA2097716C (fr) 1998-08-18
EP0560980A1 (fr) 1993-09-22
DK0560980T3 (da) 1998-08-24
US5401400A (en) 1995-03-28
US5204001A (en) 1993-04-20
TW278069B (fr) 1996-06-11
KR930703210A (ko) 1993-11-29
HU218749B (hu) 2000-11-28
AU2750592A (en) 1993-05-03
CA2097716A1 (fr) 1993-04-10

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